Design of growth‐dependent biosensors based on destabilized GFP for the detection of physiological behavior of Escherichia coli in heterogeneous bioreactors

In this work, we present the design and characterization of Green Fluorescent Protein (GFP)‐based reporter systems designed to describe cellular activity in “complex,” heterogeneous bioreactors. The reporter systems consist of Escherichia coli strains carrying growth dependent promoters fused to genes expressing stable and unstable variants of GFP, respectively. The response of Escherichia coli cells to transient exposure to glucose was studied in a two‐compartment scale down bioreactor (SDR) consisting of a well‐stirred tank reactor (STR) connected to a plug‐flow reactor (PFR). Such a SDR system is employed to mimic the situation of high glucose concentration and oxygen limitation that often encountered in large‐scale, fed‐batch bioreactors and the response of E. coli was simulated by continuously pumping microbial cells from STR to the PFR. We found that repeated addition of concentrated glucose pulses with varied frequency at the entrance of the PFR had consequences on strain physiological behavior. The GFP expressions were significantly marked after 10 h of cultivation in STR (control reactor) and SDR, whereas, growth rates were rather similar. Additional experiments in chemostat with programmed glucose perturbation suggested that the activities of the promoters were linked with the substrate limitation signal. Taken together with immunoblot analysis, we suppose protein leakage is responsible for the overexpression of fis and the related promoters, such as rrnB in this case study, but additional works are required in order to confirm this relationship. This investigation is useful for a better understanding of the fast dynamic phenomena occurring in heterogeneous large‐scale bioreactors. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 29: 553–563, 2013     

Fast dynamic response of the fermentative metabolism of Escherichia coli to aerobic and anaerobic glucose pulses

The response of Escherichia coli cells to transient exposure (step increase) in substrate concentration and anaerobiosis leading to mixed‐acid fermentation metabolism was studied in a two‐compartment bioreactor system consisting of a stirred tank reactor (STR) connected to a mini‐plug‐flow reactor (PFR: BioScope, 3.5 mL volume). Such a system can mimic the situation often encountered in large‐scale, fed‐batch bioreactors. The STR represented the zones of a large‐scale bioreactor that are far from the point of substrate addition and that can be considered as glucose limited, whereas the PFR simulated the region close to the point of substrate addition, where glucose concentration is much higher than in the rest of the bioreactor. In addition, oxygen‐poor and glucose‐rich regions can occur in large‐scale bioreactors. The response of E. coli to these large‐scale conditions was simulated by continuously pumping E. coli cells from a well stirred, glucose limited, aerated chemostat (D = 0.1 h^?1) into the mini‐PFR. A glucose pulse was added at the entrance of the PFR. In the PFR, a total of 11 samples were taken in a time frame of 92 s. In one case aerobicity in the PFR was maintained in order to evaluate the effects of glucose overflow independently of oxygen limitation. Accumulation of acetate and formate was detected after E. coli cells had been exposed for only 2 s to the glucose‐rich (aerobic) region in the PFR. In the other case, the glucose pulse was also combined with anaerobiosis in the PFR. Glucose overflow combined with anaerobiosis caused the accumulation of formate, acetate, lactate, ethanol, and succinate, which were also detected as soon as 2 s after of exposure of E. coli cells to the glucose and O₂ gradients. This approach (STR‐mini‐PFR) is useful for a better understanding of the fast dynamic phenomena occurring in large‐scale bioreactors and for the design of modified strains with an improved behavior under large‐scale conditions. Biotechnol. Bioeng. 2009; 104: 1153–1161. © 2009 Wiley Periodicals, Inc.     

Development of a predictive description of an immobilized-cell, three-phase, fluidized-bed bioreactor

A Large bioreactor is an inhomogenous system with concentration gradients which depend on the fluid dynamics and the mass transfer of the reactor, the feeding strategy, the saturation constant, and the cell density. The responses of Escherichia coli cells to short-term oscillations of the carbon/energy substrate in glucose limited fed-batch cultivations were studied in a two-compartment reactor system consisting of a stirred tank reactor (STR) and an aerated plug flow reactor (PFR) as a recycle loop. Short-term glucose excess or starvation in the PFR was simulated by feeding of glucose to the PFR or to the STR alternatively. The cellular response to repeated short-term glucose excess was a transient increase of glucose consumption and acetate formation. But, there was no accumulation of acetate in the culture, because it was consumed in the STR part where the glucose concentration was growth limiting. However, acetate accumulated during the cultivation if the oxygen supply in the PFR was insufficient, causing higher acetate formation. The biomass yield was then negatively influenced, which was also the case if the PFR was used to simulate a glucose starvation zone. The results suggest that short-term heterogeneities influence the cellular physiology and growth, and can be of major importance for the process performance. (c) 1995 John Wiley & Sons, Inc.     

A scale-down two-compartment reactor with controlled substrate oscillations: Metabolic response of Saccharomyces cerevisiae

Substrate concentration gradients are likely to appear during large scale fermentations. To study effects of such gradients on microorganisms, an aerated scale-down reactor system was constructed. It consists of a plug flow reactor (PFR) and a stirred tank reactor (STR), between which the medium is circulated. The PFR, which is an aerated static mixer reactor, was characterized with respect to plug flow behaviour and oxygen transfer. A Bodenstein number of 15–220, depending on residence time and aeration rate, and a k_La of 500–1130 h^–1, depending mainly on aeration rate, were obtained. The biological test system used, was aerobic ethanol production by Saccharomyces cerevisiae, due to sugar excess. The ethanol concentration profile and the yield of biomass were compared in two fed-batch fermentations. In the first case, the feeding point of molasses was located at the inlet of the PFR. This simulates location of the feeding point in the segregated part of a heterogeneous reactor, with local high sugar concentrations. In the second mode of operation, as a control with good mixing conditions, the PFR was disconnected from the STR, into which the substrate was fed. Differences were found: Up to 6% less biomass was produced and a larger amount of ethanol was formed in the two-compartment reactor system, due to the uneven sugar concentration distribution. This emphasizes the importance of the location of, and the mixing conditions at, the feeding point in a bioreactor.     

Further studies related to the scale-up of high cell density Escherichia coli fed-batch fermentations: the additional effect of a changing microenvironment when using aqueous ammonia to control pH

In this work, we report on the further development of the scale-down, two-compartment (STR + PFR) experimental simulation model. For the first time, the effect on high cell density Escherichia coli fed-batch fermentations of a changing microenvironment with respect to all three of the major spatial heterogeneities that may be associated with large-scale processing (pH, glucose, and dissolved oxygen concentration) were studied simultaneously. To achieve this, we used traditional microbiological analyses as well as multiparameter flow cytometry to monitor cell physiological response at the individual cell level. It was demonstrated that for E. coli W3110 under such conditions in a 20 m(3) industrial fed-batch fermentation, the biomass yield is lower and final cell viability is higher than those found in the equivalent well-mixed, 5L laboratory scale case. However, by using a combination of the well-mixed 5L stirred tank reactor (STR) with a suitable plug flow reactor (PFR) to mimic the changing microenvironment at the large scale, very similar results to those in the 20 m(3) reactor may be obtained. The similarity is greatest when the PFR is operated with a mean residence time of 50 sec with a low level of dO(2) and a high glucose concentration with either a pH of 7 throughout the two reactors or with pH controlled at 7 in the STR by addition into the PFR where the pH is > 7.     

Predicting the performance of immobilized enzyme reactors using reversible Michaelis–Menten kinetics

A general mathematical model is developed in the present work for predicting the steady state performance of immobilized enzyme reactor performing reversible Michaelis - Menten kinetics. The model takes into account the effect of external diffusional limitations, the axial dispersion and the equilibrium constant on reactor performance quantified as relative substrate conversion and yield. The performance of reactor is characterized using the dimensionless parameters of Damkohler number, Stanton number, Peclet number, the equilibrium constant and the dimensionless input substrate concentration. The reactor performance is described for the two extreme cases of plug flow reactor (PFR) and continuous stirred tank reactor (CSTR) in addition to the intermediate case of dispersed plug flow reactor (DPFR). The performance of reactor is compared for the two cases of zero order and reversible first order kinetics.     

Microbially enhanced chemisorption of nickel into biologically synthesized hydrogen uranyl phosphate: a novel system for the removal and recovery of metals from aqueous solutions

Ni(2+) was removed quantitatively from aqueous flows by columns loaded with polycrystalline hydrogen uranyl phosphate (HUP) bound to immobilized cells of Citrobacter sp. The columns functioned effectively in Ni uptake/regeneration cycles; five cycles were completed without significant decrease in the Ni-removing capacity of the column. The influence of pH, temperature, and flow rate on the Ni-removing capacity of the columns was examined. The composition of the Ni/HUP cell-bound deposits was confirmed by X-ray diffraction analysis (XRD) and proton-induced X-ray emission (PIXE) spectroscopy following several consecutive metal challenges and is discussed in relation to the mechanism of Ni(2+) removal from solution via ion-exchange intercalation into the interlayer space of HUP. Ni was selectively recovered from the columns using citrate or tartrate. The regenerated columns functioned effectively in Ni removal throughout repeated Ni challenge and desorption cycles. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 54: 319-328, 1997.     

A two-compartment bioreactor system made of commercial parts for bioprocess scale-down studies: impact of oscillations on Bacillus subtilis fed-batch cultivations

This study describes an advanced version of a two-compartment scale-down bioreactor that simulates inhomogeneities present in large-scale industrial bioreactors on the laboratory scale. The system is made of commercially available parts and is suitable for sterilization with steam. The scale-down bioreactor consists of a usual stirred tank bioreactor (STR) and a plug flow reactor (PFR) equipped with static mixer modules. The PFR module with a working volume of 1.2 L is equipped with five sample ports, and pH and dissolved oxygen (DO) sensors. The concept was applied using the non-sporulating Bacillus subtilis mutant strain AS3, characterized by a SpoIIGA gene knockout. In a fed-batch process with a constant feed rate, it is found that oscillating substrate and DO concentration led to diminished glucose uptake, ethanol formation and an altered amino acid synthesis. Sampling at the PFR module allowed the detection of dynamics at different concentrations of intermediates, such as pyruvic acid, lactic acid and amino acids. Results indicate that the carbon flux at excess glucose and low DO concentrations is shifted towards ethanol formation. As a result, the reduced carbon flux entering the tricarboxylic acid cycle is not sufficient to support amino acid synthesis following the oxaloacetic acid branch point.     

Lactic acid fermentation in a recycle batch reactor using immobilized Lactobacillus casei

Lactic acid production by recycle batch fermentation using immobilized cells of Lactobacillus casei subsp. rhamnosus was studied. The culture medium was composed of whey treated with an endoprotease, and supplemented with 2.5 g/L of yeast extract and 0.18 mM Mn(2+) ions. The fermentation set-up comprised of a column packed with polyethyleneimine-coated foam glass particles, Pora-bact A, and connected with recirculation to a stirred tank reactor vessel for pH control. The immobilization of L. casei was performed simply by circulating the culture medium inoculated with the organism over the beads. At this stage, a long lag period preceded the cell growth and lactic acid production. Subsequently, for recycle batch fermentations using the immobilized cells, the reducing sugar concentration of the medium was increased to 100 g/L by addition of glucose. The lactic acid production started immediately after onset of fermentation and the average reactor productivity during repeated cycles was about 4.3 to 4.6 g/L . h, with complete substrate utilization and more than 90% product yield. Sugar consumption and lactate yield were maintained at the same level with increase in medium volume up to at least 10 times that of the immobilized biocatalyst. The liberation of significant amounts of cells into the medium limited the number of fermentation cycles possible in a recycle batch mode. Use of lower yeast extract concentration reduced the amount of suspended biomass without significant change in productivity, thereby also increasing the number of fermentation cycles, and even maintained the D-lactate amount at low levels. The product was recovered from the clarified and decolorized broth by ion-exchange adsorption. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 55:841-853, 1997.     

Inhibition kinetics of phenol degradation from unstable steady-state data

Multiplicity of steady states of a continuous culture with an inhibitory substrate was used to estimate kinetic parameters under steady-state conditions. A continuous culture of Pseudomonas cepacia G4, using phenol as the sole source of carbon and energy, was overloaded by increasing the dilution rate above the critical dilution rate. The culture was then stabilized in the inhibitory branch by a proportional controller using the carbon dioxide concentration in the reactor exhaust gas as the controlled variable and the dilution rate as the manipulated variable. By variation of the set point, several unstable steady states in the inhibitory branch were investigated and the specific phenol conversion rates calculated. In addition, phenol degradation was investigated under substrate limitation (chemostat operation).The results show that the phenol degradation by P. cepacia can be described by the same set of inhibition parameters under substrate limitation and under high substrate concentrations in the inhibitory branch. Biomass yield and maintenance coefficients were identical. Fitting of the data to various inhibition models resulted in the best fit for the Yano and Koga equation. The well-known Haldane model, which is most often used to describe substrate inhibition by phenol, gave the poorest fit. The described method allows a precise data estimation under steady-state conditions from the maximum of the biological reaction rate up to high substrate concentrations in the inhibitory branch. Inhibition parameter estimation by controlling unstable steady states may thus be useful in avoiding discrepancies between data generated by batch runs and their application to continuous cultures which have been often described in the literature. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 54: 567-576, 1997.     

Scale-down model to simulate spatial pH variations in large-scale bioreactors

For the first time a laboratory-scale two-compartment system was used to investigate the effects of pH fluctuations consequent to large scales of operation on microorganisms. pH fluctuations can develop in production-scale fermenters as a consequence of the combined effects of poor mixing and adding concentrated reagents at the liquid surface for control of the bulk pH. Bacillus subtilis was used as a model culture since in addition to its sensitivity to dissolved oxygen levels, the production of the metabolites, acetoin and 2,3-butanediol, is sensitive to pH values between 6.5 and 7.2. The scale-down model consisted of a stirred tank reactor (STR) and a recycle loop containing a plug flow reactor (PFR), with the pH in the stirred tank being maintained at 6.5 by addition of alkali in the loop. Different residence times in the loop simulated the exposure time of fluid elements to high values of pH in the vicinity of the addition point in large bioreactors and tracer experiments were performed to characterise the residence time distribution in it. Since the culture was sensitive to dissolved oxygen, for each experiment with pH control by adding base into the PFR, equivalent experiments were conducted with pH control by addition of base into the STR, thus ensuring that any dissolved oxygen effects were common to both types of experiments. The present study indicates that although biomass concentration remained unaffected by pH variations, product formation was influenced by residence times in the PFR of 60 sec or longer. These changes in metabolism are thought to be linked to both the sensitivity of the acetoin and 2,3-butanediol-forming enzymes to pH and to the inducing effects of dissociated acetate on the acetolactate synthase enzyme.     

Cadmium accumulation by a Citrobacter sp. immobilized on gel and solid supports: Applicability to the treatment of liquid wastes containing heavy metal cations

Polyacrylamide gel-immobilized cells of a Citrobacter sp. removed cadmium from flows supplemented with glycerol 2-phosphate, the metal uptake mechanism being mediated by the activity of a cell-bound phosphatase that precipitates liberated inorganic phosphate with heavy metals at the cell surface. The constraints of elevated flow rate and temperature were investigated and the results discussed in terms of the kinetics of immobilized enzymes. Loss in activity with respect to cadmium accumulation but not inorganic phosphate liberation was observed at acid pH and was attributed to the pH-dependent solubility of cadmium photsphate. Similarly high concentrations of chloride ions, and traces of cyanide inhibited cadmium uptake and this was attributed to the ability of these anions to complex heavy metals, especially the ability of CN(-) to form complex anions with Cd(2+). The data are discussed in terms of the known chemistry of chloride and cyanide-cadmium complexes and the relevance of these factors in the treatment of metal-containing liquid wastes is discussed. The cells immobilized in polyacrylamide provided a convenient small-scale laboratory model system. It was found that the Citrobacter sp. could be immobilized on glass supports with no chemical treatment or modification necessary. Such cells were also effective in metal accumulation and a prototype system more applicable to the treatment of metal-containing streams on a larger scale is described.     

Enzymatic saccharification of sugar cane bagasse by continuous xylanase and cellulase production from cellulomonas flavigena PR‐22

Cellulase (CMCase) and xylanase enzyme production and saccharification of sugar cane bagasse were coupled into two stages and named enzyme production and sugar cane bagasse saccharification. The performance of Cellulomonas flavigena (Cf) PR‐22 cultured in a bubble column reactor (BCR) was compared to that in a stirred tank reactor (STR). Cells cultured in the BCR presented higher yields and productivity of both CMCase and xylanase activities than those grown in the STR configuration. A continuous culture with Cf PR‐22 was run in the BCR using 1% alkali‐pretreated sugar cane bagasse and mineral media, at dilution rates ranging from 0.04 to 0.22 1/h. The highest enzymatic productivity values were found at 0.08 1/h with 1846.4 ± 126.4 and 101.6 ± 5.6 U/L·h for xylanase and CMCase, respectively. Effluent from the BCR in steady state was transferred to an enzymatic reactor operated in fed‐batch mode with an initial load of 75 g of pretreated sugar cane bagasse; saccharification was then performed in an STR at 55°C and 300 rpm for 90 h. The constant addition of fresh enzyme as well as the increase in time of contact with the substrate increased the total soluble sugar concentration 83% compared to the value obtained in a batch enzymatic reactor. This advantageous strategy may be used for industrial enzyme pretreatment and saccharification of lignocellulosic wastes to be used in bioethanol and chemicals production from lignocellulose. © 2016 American Institute of Chemical Engineers Biotechnol. Prog., 32:321–326, 2016     

Tc(VII) reduction and accumulation by immobilized cells of Escherichia coli

Resting cells of Escherichia coli, immobilized in a flow-through bioreactor, coupled the oxidation of formate or hydrogen to Tc(VII) reduction and removal from solution. Cells, pregrown anaerobically in a hollow-fiber membrane bioreactor, were challenged with 50 muM Tc(VII) in a carrier solution of phosphate-buffered saline. The radionuclide accumulated within the membrane component of the reactor, corresponding to the localization of the cells. Negligible Tc removal was noted in a reactor containing a mutant deficient in active Tc(VII) reductase, when supplied with formate as an electron donor. Formate or hydrogen was supplied as the electron donor for Tc(VII) reduction to cells immobilized in reactors operated in transverse (crossflow) and direct (dead-end filtration) modes, respectively. Flow-rate activity relationships were used to compare the performance of the reactors. A flow rate of 2.4 mL h(-1) supported the removal of 50% of the Tc from solution in a reactor operated in transverse mode with formate as an electron donor. In contrast, a flow rate of 0.7 mL h(-1), supported comparable Tc removal when hydrogen was introduced to a reactor operated in direct mode. The reduced reactor efficiency, when hydrogen was used as an electron donor, could be attributed, in part, to poor delivery of the gas to the cells. The biocatalyst was highly stable in the reactor; no loss in activity was noted over 200 h of continuous use. (c) 1997 John Wiley & Sons Inc. Biotechnol Bioeng 55: 505-510, 1997.     

Phosphate release and heavy metal accumulation by biofilm-immobilized and chemically-coupled cells of a Citrobacter sp. pre-grown in continuous culture

A heavy metal-accumulating Citrobacter sp. was grown in carbon-limiting continuous culture in an air-lift fermentor containing raschig rings as support for biofilm development. Planktonic cells from the culture outflow were immobilized in parallel on raschig rings by chemical coupling (silanization), for quantitative comparison of phosphatase activity and uranyl uptake by both types of immobilized cell. The flow rate giving 50% conversion of substrate to product (phosphate) in flow-through reactors was higher, by 35-40%, for the biofilm-immobilized cells, possibly exploiting a pH-buffering effect of inorganic phosphate species within the extracellular polymeric material. Upon incorporation of uranyl ions (0.2 mM UO22+), both types of cell removed more than 90% of the input UO22+ at slow flow rates, but the chemically-coupled cells performed better at higher flow rates. The deposited material (HUO2PO4) subsequently removed Ni2+ from a second flow via intercalative ion exchange of Ni2+ into the crystalline HUO2PO4.4H2O lattice. This occurred irrespective of the method of coupling of the biomass to the support and suggested that uranyl phosphate accumulated by both types of cell has potential as a bio-inorganic ion exchanger-a potential use for the uranium recoved from primary waste treatment processes.     

Continuous production of maltotetraose using immobilized Pseudomonas stutzeri amylase

A continuous production process of maltotetraose was investigated by using immobilized maltotetraose (G(4))- forming amylase (1,4-alpha-D-glucan maltotetraohydrolase, EC3.2.1.60) from Pseudomonas stutzeri adsorbed on a macroporous hydrophobic resin. The maximum reaction rate was obtained at 55 degrees C and the activation energy of hydrolysis by immobilized G(4)-forming amylase was calculated to be 8.45 kcal/mol. The maltotetraose yield was greatly influenced by the flow rate of substrate solution, its concentration, and the immobilized enzyme activity. The newly defined factor "specific space velocity" was successfully introduced to normalize the operating parameters. Using this factor, the immobilized enzyme reactor then can be simulated and the operating dynamics can be determined.     

An immobilized cell reactor with simultaneous product separation. I. Reactor design and analysis

A four-phase reactor-separator (gas, liquid, solid, and immobilized catalyst) is proposed for fermentations characterized by a volatile product and nonvolatile substrate.In this reactor, the biological catalyst is immobilized onto a solid column packing and contacted by the liquid containing the substrate.A gas phase is also moved through the column to strip the volatile product into the gas phase. The Immobilized Cell Reactor-Separator (ICRS) consists of two basic gas-liquid flow sections: a cocurrent "enricher" followed by a countercurrent-"stripper".In this article, an equilibrium stage model of the reactor is developed to determine the feasibility and important operational variables of such a reactor-separator. The ICRS concept is applied to the ethanol from whey lactose fermentation using some preliminary immobilized cell reactor performance data. A mathematical model for a steady-state population based on an adsorbed monolayer of cells is also developed for the reactor. The ICRS model demonstrated that the ICRS should give a significant increase in reactor productivity as compared to an identically sized Immobilized Cell Reactor (ICR) with no separation. The gas-phase separation of the product also allows fermentation of high inlet substrate concentrations. The model is used to determine the effects of reactor parameters on ICRS performance including temperature, pressure, gas flow rates, inlet substrate concentration, and degree of microbial product inhibition.     

Kinetic studies on hybridoma cells immobilized in fixed bed reactors

Cultures with immobilized hybridoma cells were performed in fixed bed systems. "Steady state" values for volume-specific substrate uptake and metabolite production rates were determined at various perfusion rates and superficial flow velocities of the medium within the carrier matrix. Data from fixed bed volumes between 50 and 600 ml did not show any difference. The volume-specific glutamine and glucose uptake rate turned out to be independent of the superficial flow velocity, but decreased with decreasing glutamine and glucose concentration. The volume-specific oxygen uptake rate increased with increasing superficial flow velocity and substrate concentration, respectively. A similar behavior was observed for the ratio between oxygen and glucose uptake rate. The production rate for monoclonal antibodies was neither affected by the substrate concentration nor by the superficial flow velocity. The metabolic parameters of the immobilized cells were put into kinetic equations and compared to those of suspended cells. It could be concluded that the metabolism of the immobilized cells is determined by the oxygen supply within the macroporous carriers. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 55: 535-541, 1997.     

Immobilization of penicillin G acylase on aminoalkylated polyacrylic supports

A procedure is described for the immobilization of penicillin G acylase (PA) on Amberlite XAD7 modified by transamidation with 1,2-ethylenediamine and activated with glutaraldehyde. Reduction with sodium borohydride of the Schiff's bases formed between the amino groups of the protein and glutaraldehyde results in a dramatic improvement of the operational stability of the immobilized enzyme without affecting the catalytic activity. The enzyme kept in presence of the substrate, penicillin G, displays an increased stability with respect to that stored in pure phosphate buffer solution. The inactivation kinetics of the immobilized preparations of PA, determined in a continuous fixed bed reactor, as well as a discontinuous batch reactor, are reported.     

Entrapment of lipase into K-carrageenan beads and its use in hydrolysis of olive oil in biphasic system

The porcine pancrease lipase was immobilized by entrapment in the beads of K-carrageenan and cured by treatment with polyethyleneimine (PEI) in the phosphate buffer. The retention of hydrolytic activity of lipase and compressive strength of the beads were examined. The activity of free and immobilized lipase was assessed by using olive oil as the substrate. The immobilized enzyme exhibited a little shift towards acidic pH for its optimal activity and retained 50% of its activity after 5 cycles. When the enzyme concentration was kept constant and substrate concentration was varied the K_m and V_max were observed to be 0.18 × 10⁻² and 0.10, and 0.10 × 10⁻² and 0.09 respectively, for free and for entrapped enzymes. When the substrate concentration was kept constant and enzyme concentration was varied, the values of K_m and V_max were observed to be 0.19 × 10⁻⁷ and 0.41, and 0.18 × 10⁻⁷ and 0.41 for free and entrapped enzymes. Though this indicates that there is no conformational change during immobilization, it also shows that the reaction velocity depends on the concentration. Immobilized enzyme showed improved thermal and storage stability. Hydrolysis of olive oil in organic–aqueous two-phase system using fixed bed reactor was carried out and conditions were optimized. The enzyme in reactor retained 30% of its initial activity after 480 min (12 cycles).